CN1256180C - Separated regulatable quasi-fluidized bed reactor - Google Patents
Separated regulatable quasi-fluidized bed reactor Download PDFInfo
- Publication number
- CN1256180C CN1256180C CN200410014229.7A CN200410014229A CN1256180C CN 1256180 C CN1256180 C CN 1256180C CN 200410014229 A CN200410014229 A CN 200410014229A CN 1256180 C CN1256180 C CN 1256180C
- Authority
- CN
- China
- Prior art keywords
- tower body
- split type
- liquid
- gas
- diversing bucket
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
- 239000007787 solid Substances 0.000 claims abstract description 44
- 239000007788 liquid Substances 0.000 claims abstract description 39
- 238000006243 chemical reaction Methods 0.000 claims abstract description 14
- 238000005243 fluidization Methods 0.000 claims abstract description 6
- 239000008187 granular material Substances 0.000 claims abstract description 5
- 239000012071 phase Substances 0.000 claims description 26
- 238000011068 loading method Methods 0.000 claims description 8
- 239000007791 liquid phase Substances 0.000 claims description 6
- 239000003054 catalyst Substances 0.000 claims description 4
- 230000009183 running Effects 0.000 claims description 4
- 239000000126 substance Substances 0.000 abstract description 3
- 238000006555 catalytic reaction Methods 0.000 abstract description 2
- 239000007789 gas Substances 0.000 abstract 4
- 238000004062 sedimentation Methods 0.000 abstract 1
- KKEYFWRCBNTPAC-UHFFFAOYSA-N Terephthalic acid Chemical compound OC(=O)C1=CC=C(C(O)=O)C=C1 KKEYFWRCBNTPAC-UHFFFAOYSA-N 0.000 description 14
- VZCYOOQTPOCHFL-OWOJBTEDSA-N Fumaric acid Chemical compound OC(=O)\C=C\C(O)=O VZCYOOQTPOCHFL-OWOJBTEDSA-N 0.000 description 12
- 239000002245 particle Substances 0.000 description 10
- 239000002351 wastewater Substances 0.000 description 10
- 239000001530 fumaric acid Substances 0.000 description 6
- 239000000463 material Substances 0.000 description 6
- VZCYOOQTPOCHFL-UHFFFAOYSA-N trans-butenedioic acid Natural products OC(=O)C=CC(O)=O VZCYOOQTPOCHFL-UHFFFAOYSA-N 0.000 description 6
- 238000005265 energy consumption Methods 0.000 description 5
- 238000012546 transfer Methods 0.000 description 5
- 238000012423 maintenance Methods 0.000 description 4
- 230000001105 regulatory effect Effects 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- 238000009825 accumulation Methods 0.000 description 3
- 230000001580 bacterial effect Effects 0.000 description 3
- 230000005587 bubbling Effects 0.000 description 3
- 238000004043 dyeing Methods 0.000 description 3
- 238000000034 method Methods 0.000 description 3
- 238000007639 printing Methods 0.000 description 3
- 238000012545 processing Methods 0.000 description 3
- 238000003746 solid phase reaction Methods 0.000 description 3
- PAYRUJLWNCNPSJ-UHFFFAOYSA-N Aniline Chemical compound NC1=CC=CC=C1 PAYRUJLWNCNPSJ-UHFFFAOYSA-N 0.000 description 2
- 230000002950 deficient Effects 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000012467 final product Substances 0.000 description 2
- 235000013305 food Nutrition 0.000 description 2
- 239000007790 solid phase Substances 0.000 description 2
- QTBSBXVTEAMEQO-UHFFFAOYSA-M Acetate Chemical compound CC([O-])=O QTBSBXVTEAMEQO-UHFFFAOYSA-M 0.000 description 1
- MQIUGAXCHLFZKX-UHFFFAOYSA-N Di-n-octyl phthalate Natural products CCCCCCCCOC(=O)C1=CC=CC=C1C(=O)OCCCCCCCC MQIUGAXCHLFZKX-UHFFFAOYSA-N 0.000 description 1
- 102000004190 Enzymes Human genes 0.000 description 1
- 108090000790 Enzymes Proteins 0.000 description 1
- XBDQKXXYIPTUBI-UHFFFAOYSA-M Propionate Chemical compound CCC([O-])=O XBDQKXXYIPTUBI-UHFFFAOYSA-M 0.000 description 1
- 229920002472 Starch Polymers 0.000 description 1
- KXKVLQRXCPHEJC-UHFFFAOYSA-N acetic acid trimethyl ester Natural products COC(C)=O KXKVLQRXCPHEJC-UHFFFAOYSA-N 0.000 description 1
- PYKYMHQGRFAEBM-UHFFFAOYSA-N anthraquinone Natural products CCC(=O)c1c(O)c2C(=O)C3C(C=CC=C3O)C(=O)c2cc1CC(=O)OC PYKYMHQGRFAEBM-UHFFFAOYSA-N 0.000 description 1
- 150000004056 anthraquinones Chemical class 0.000 description 1
- 239000011942 biocatalyst Substances 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- BJQHLKABXJIVAM-UHFFFAOYSA-N bis(2-ethylhexyl) phthalate Chemical compound CCCCC(CC)COC(=O)C1=CC=CC=C1C(=O)OCC(CC)CCCC BJQHLKABXJIVAM-UHFFFAOYSA-N 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 238000010523 cascade reaction Methods 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 239000012295 chemical reaction liquid Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000008520 organization Effects 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 238000005191 phase separation Methods 0.000 description 1
- 102000004169 proteins and genes Human genes 0.000 description 1
- 108090000623 proteins and genes Proteins 0.000 description 1
- 235000019698 starch Nutrition 0.000 description 1
- 239000008107 starch Substances 0.000 description 1
Images
Landscapes
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The present invention relates to a split adjustable quasi-fluidized bed reactor, particularly to a novel split adjustable quasi-fluidized bed reactor for various air-liquid-solid three phase reactions, which belongs to the fields of environment, biology and chemical industry. The reactor comprises a split tower body, a diversion barrel, a gas distributor, an air-liquid-solid three phase separator, a viewing mirror, a diversion barrel adjusting rod, liquid connection pipelines between towers, gas connection pipelines between towers, a solid discharge outlet and a liquid discharge outlet, wherein the adjustable diversion barrel is arranged in the split tower body. The upper end of the diversion barrel is provided with the diversion barrel adjusting rod; the upper part of the split adjustable tower body is provided with the air-liquid-solid three phase separator; the lower part of the split tower body is provided with the gas distributor which can be freely dismounted. The split tower body can be one or more; each tower body can singly run, and can be singly loaded with catalysis granules of different types and different quantity according to operation conditions and filled with different reaction gases and liquids. Meanwhile, the fluidization regions and the sedimentation regions of single tower body can be freely adjusted.
Description
Technical field
What a kind of split type adjustable plan fluidized-bed reactor of the present invention related to is a kind of novel split type adjustable plan fluidized-bed reactor that is used for all kinds of gas-liquid-solid phase reactions, belongs to environment, biology and chemical field.
Background technology
Present gas-liquid-solid phase reactor is widely used in environmental project, in bioengineering, Chemical Engineering and other industrial process.Usually, gas-liquid-solid phase reaction all adopts bubbling style reactor or stirred-tank reactor.This two quasi-traditions reactor efficiency is low, the energy consumption height, and application is subjected to the restriction of reaction system.Effective mixing of gas-liquid-solid three-phase in these courses of reaction, mass-transfer efficiency, operating flexibility and effective the maintenance are the important performances of reactor.
The interior circular flow reactor that grows up based on bubbling style reactor is to introduce diversing bucket in reactor, be that fluid produces in reactor and circulates, thereby strengthened gas-liquid-solid three-phase mixed effect, the overall mass transfer rate of reactor also is higher than traditional bubbling style reactor.
But, traditional common loop reactor exists several serious defectives, the ratio of internal diameter that is the diameter of diversing bucket and reactor is constant, the fixed-site of diversing bucket in reactor, in case reactor machines the character and the operating condition of the fluidisation area that just is difficult to change largely reactor and settling zone, gas-liquid-solid three-phase, operating flexibility is lower.In addition, because the ratio of height to diameter of traditional common loop reactor is had relatively high expectations, amplify for industry and bring difficulty.When the gas-liquid-solid three-phase common loop reactor of large-scale integral type moved, energy consumption was higher, complex structure, and bubble merging is bigger, and operating flexibility is low, and maintenance cost is higher.
Summary of the invention
The objective of the invention is provides a kind of split type adjustable plan fluidized-bed reactor at the weak point that above-mentioned traditional gas-liquid-solid three-phase common loop reactor of integral type exists, this novel split type adjustable plan fluidized-bed reactor has adopted split type tower body, adjustable flexibly solar term liquid connecting line and can freely regulated diversing bucket has solved fully that the gas-liquid-solid three-phase common loop reactor of traditional integral type energy consumption is higher, complex structure, operating flexibility is low, maintenance cost is higher defective; Its hydrodynamic performance is good, mass transfer rate is high and mixing of materials is abundant.Owing to adopted split type tower body, can in the single tower body of reactor, load the catalyst granules of dissimilar and different loadings as requested, feed the reacting gas and the liquid of heterogeneity and different in flow rate and pressure.Reactor start-up is very fast, and it is shorter to reach the normal service requirement time, and gas merger property is less; Adjustable flexibly solar term liquid connecting line and can regulate the diversing bucket of diameter, length and position can free adjustment the fluidisation area and the settling zone of adjustable plan fluidized-bed reactor, make that the reactor energy consumption is low, easy to process, reactor material requires lower, operating flexibility is big, safeguard simply, can be widely used in all kinds of gas-liquid-solid phase reaction processes.
A kind of split type adjustable plan fluidized-bed reactor takes following scheme to realize: split type adjustable plan fluidized-bed reactor structure comprises between split type tower body, diversing bucket, gas distributor, gas-liquid-solid three phase separator, visor, diversing bucket adjusting rod, tower gas connection pipe line, solid discharge mouth, liquid discharge outlet between liquid connecting line, tower.Adjustable diversing bucket is housed in the split type tower body, the diversing bucket upper end is equipped with the diversing bucket adjusting rod, the gas distributor of detachable is equipped with in the bottom of split type tower body, gas-liquid-solid three phase separator is equipped with on the top of split type adjustable tower body, on the split type tower body visor is housed, split type tower body lower device has solid discharge mouth, liquid discharge outlet.
Split type tower body can be one or more tower bodies, and each tower body can both isolated operation or a plurality of tower body combined running.Device has liquid connecting line, a plurality of liquid control valve door between the tower body of split type adjustable tower body, and device has gas connection pipe line, a plurality of gas control valve between the tower body of split type tower body.
The characteristics of the novel split type adjustable plan fluidized-bed reactor of the present invention are:
The novel split type adjustable plan fluidized-bed reactor of the present invention by between split type tower body, diversing bucket, gas distributor, gas-liquid-solid three phase separator, visor, diversing bucket adjusting rod, tower between liquid connecting line, tower gas connection pipe line, solid discharge mouth, liquid discharge outlet constitute, project organization is simple, and operability is good.
2. split type adjustable tower body is one or more tower bodies, each tower body can both move individually, can load catalyst granules, the different reacting gas and the reaction liquids of feeding of dissimilar and different loadings according to operating condition separately, and the fluidisation area and the settling zone of the single tower body of free adjustment.Reactor start-up is very fast, and it is shorter to reach the normal service requirement time, and energy consumption is lower, and is easy to process, and reactor material requires lower.
3. the gas distributor of detachable is equipped with in the bottom of the single tower body of split type tower body, reacting gas enters tower body through gas distributor, bubble at the single tower body of split type tower body once generation, because the jet power and the density contrast of gas, the liquid that bubble group will drive in the diversing bucket moves upward, drive moving upward of solid particle simultaneously, solid particle is evenly distributed in reactor, and local accumulation does not take place; The mass-transfer efficiency height, mixing of materials is abundant.
4. the diversing bucket of the single tower body of split type tower body upper end is equipped with the diversing bucket adjusting rod, and adjusting rod is 2 screw rods, can radially freely regulated diversing bucket position and the size and the diameter of diversing bucket, and when changing, reactor operating condition make reactor working properly.
5. the liquid between the single tower body of split type tower body can be carried by liquid connecting line between tower; By regulating different Inlet and outlet water valves, can make single tower body free conversion between in parallel or series connection of split type tower body, but and the liquid phase hydraulic detention time of the single tower body of free adjustment.Gas between the single tower body of split type adjustable tower body can be carried by gas connection pipe line between tower; By regulating different air intake valves, can make the gas free conversion between gas of different nature in the single tower body of split type adjustable tower body, but and the air inflow of the single tower body of free adjustment and pressure; The reactor operating flexibility is bigger.
Description of drawings
Below with reference to accompanying drawing the split type adjustable plan fluidized-bed reactor of the present invention is described further.
Fig. 1 is the main structure chart (comprising 3 tower bodies with split type tower body is example) of the split type adjustable plan fluidized-bed reactor of the present invention.
Fig. 2 is the diversing bucket adjusting rod structure chart of the single tower body of the split type adjustable plan fluidized-bed reactor of the present invention.
Fig. 3 is the gas distributor structure chart of the single tower body of the split type adjustable plan fluidized-bed reactor of the present invention.
Fig. 4 is the gas-liquid-solid three phase separator structure chart of the single tower body of the split type adjustable plan fluidized-bed reactor of the present invention.
Fig. 5 is the skimming baffle schematic diagram of the gas-liquid-solid three phase separator of the single tower body of the split type adjustable plan fluidized-bed reactor of the present invention.
Fig. 6 is the visor structure chart of the single tower body of the split type adjustable plan fluidized-bed reactor of the present invention;
Fig. 7 is liquid connecting line structure for conveying figure (comprising 3 tower bodies with split type tower body is example) between the tower of the split type adjustable plan fluidized-bed reactor of the present invention;
Fig. 8 is gas connection pipe line structure for conveying figure (comprising 3 tower bodies with split type tower body is example) between the tower of the split type adjustable plan fluidized-bed reactor of the present invention;
Fig. 9 is the solid discharge mouth and the liquid discharge outlet structure chart of the single tower body of the split type adjustable plan fluidized-bed reactor of the present invention;
Figure 10 is the fluidized state figure of the single tower body of the split type adjustable plan fluidized-bed reactor of the present invention.
The specific embodiment
With reference to accompanying drawing 1～10, a kind of split type adjustable plan fluidized-bed reactor structure comprises split type tower body 1, diversing bucket 2, gas distributor 3, gas-liquid-solid three phase separator 4, visor 5, diversing bucket adjusting rod 6, liquid connecting line 7 between tower, gas connection pipe line 8 between tower, solid discharge mouth 9, liquid discharge outlet 10.In the split type tower body 1 diversing bucket 2 is housed, diversing bucket 2 upper ends are equipped with diversing bucket adjusting rod 6, the gas distributor 3 of detachable is equipped with in the bottom of split type tower body 1, gas-liquid-solid three phase separator 4 is equipped with on the top of split type tower body 1, on the split type tower body 1 visor 5 is housed, split type tower body 1 lower device has solid discharge mouth 9, liquid discharge outlet 10.
Split type tower body can be one or more tower bodies, and each tower body can both isolated operation or a plurality of tower body combined running.Device has liquid connecting line, a plurality of liquid control valve door between the tower body of split type tower body, and device has gas connection pipe line, a plurality of gas control valve between the tower body of split type tower body.
As shown in Figure 1, split type adjustable tower body is one or more tower bodies (comprising 3 tower bodies with split type adjustable tower body among the figure is example), the height overall of the single tower body of split type tower body is 6-12 with the ratio of the internal diameter of single tower body, but all isolated operations of each tower body, the catalyst granules of dissimilar and different loadings be can load according to operating condition separately, different reacting gas and liquid fed.
As shown in Figure 2, diversing bucket 2 diameters of the single tower body of split type tower body are 0.3-0.6 with the ratio of the internal diameter of single tower body.Diversing bucket 2 upper ends of the single tower body of split type tower body are equipped with diversing bucket adjusting rod 6; The diversing bucket adjusting rod is 2 screw rods, and diversing bucket adjusting rod 6 tops are connected with gas-liquid-solid three phase separator 4, radially the size of free adjustment length and diversing bucket and diameter.When reactor operating condition changes, the length of the adjusting rod by suitable adjusting diversing bucket, change the position of diversing bucket in tower body, or change diversing bucket where necessary, change the ratio of diversing bucket diameter and the internal diameter of single tower body, regulate the fluidisation area and the settling zone of single tower body, thereby make reactor obtain desired duty.
Shown in accompanying drawing 3,10, the gas distributor 3 of the single tower body of split type tower body is installed on the bottom of tower body, detachable, and the distance of the following end distance gas distributor 3 of the diversing bucket 2 of the single tower body of split type tower body is 0.5-1.5 with interior diversing bucket 2 diameter ratios.Reacting gas enters through gas distributor 3 in the tower body bottom, around gas distributor, evenly produce a large amount of bubbles immediately, also promptly around gas distributor, form rare phase region, the density of dilute-phase zone is less than liquid on every side, under density contrast and gas enter momentum effect in the reactor, in the diversing bucket moved upward inside, the liquid and the solid of diversing bucket 2 outsides move downward bubble, form circulation together with the liquid of dilute-phase zone and solid.Gas is the solubility height in liquid phase, and solid particle is evenly distributed in reactor, and local accumulation does not take place, reactor inner transmission matter efficient height, and mixing of materials is abundant.
Shown in accompanying drawing 4,5, the gas-liquid-solid three phase separator 4 of the single tower body of a kind of split type adjustable plan fluidized-bed reactor is installed on the top of tower body, porous skimming baffle 23 is installed, and the distance of the gas-liquid-solid three phase separator 4 of upper end distance of diversing bucket 2 is 1-3 with interior diversing bucket 2 diameter ratios.This design can make the gas-liquid-solid three-phase in the reactor separate timely and effectively on the top of tower body, and solid phase moves downward with liquid phase, and gas phase separation is outside tower, and the part of liquid phase is isolated tower body by the control of valve.
As shown in Figure 6, the single tower body of a kind of split type adjustable plan fluidized-bed reactor is installed visor 5 in two ends up and down; The lower end visor is 0.5-1 apart from the distance of gas distributor 3 upper ends with interior diversing bucket 2 diameter ratios, and the upper end visor is 1-1.5 apart from the distance of gas-liquid-solid three phase separator 4 with interior diversing bucket 2 diameter ratios.
As shown in Figure 7, liquid connecting line between a kind of tower of split type adjustable plan fluidized-bed reactor (comprising 3 tower bodies with split type tower body is example) is by a plurality of valve controls, can make single tower body free conversion between in parallel or series connection of split type adjustable plan fluidized-bed reactor, but and the liquid phase hydraulic detention time of the single tower body of free adjustment.During in parallel reaction, only need open valve 1 ', 4 ', 5 ', 6 ', 7 ', 8 ', 9 ', 10 ', valve-off 2 ', 3 ' get final product.During cascade reaction, only need open valve 1 ', 2 ', 3 ', 6 ', 7 ', 10 ', valve-off 4 ', 5 ', 8 ', 9 ' get final product.
As shown in Figure 8, device has the gas connection pipe line between the tower body of the split type tower body of gas connection pipe line structure for conveying figure between the tower of novel split type adjustable plan fluidized-bed reactor (comprising 3 tower bodies with split type tower body is example), a plurality of gas control valves, the gas between the single tower body of split type adjustable tower body can be carried by gas connection pipe line between tower; Pass through control valve, make the gas free conversion between gas of different nature in the single tower body of split type tower body, and the air inflow and the pressure of the single tower body of energy free adjustment, by a plurality of valve 11,12,13,14,15,16 controls, can make the gas free conversion between gas of different nature in the single tower body of split type adjustable tower body, regulate the air intake valve size simultaneously, observe the charge flow rate meter, the single tower body of novel split type adjustable plan fluidized-bed reactor is worked under different charge flow rates.
As shown in Figure 9, a kind of single tower body bottom of split type adjustable plan fluidized-bed reactor all is equipped with liquid discharge outlet and solid discharge mouth.Control valve 17,18,19 can be discharged the liquid in the reactor wholly or in part, and control valve 20,21,22 can be discharged the solid in the reactor wholly or in part.This design, not only convenient charging and blowing make things convenient for simultaneously at the integral reactor running hours single tower body are carried out maintenance and debugging.
As shown in Figure 10, a kind of single tower body fluidized state of split type adjustable plan fluidized-bed reactor, reacting gas enters tower body through gas distributor, bubble at the single tower body of split type tower body once generation, because the jet power and the density contrast of gas, the liquid that bubble group will drive in the diversing bucket moves upward, and drives moving upward of solid particle simultaneously, solid particle is evenly distributed in reactor, and local accumulation does not take place.The mass-transfer efficiency height, mixing of materials is abundant.
Introduce several specific embodiment of the present invention below:
Embodiment 1: the processing of high concentration terephthalic acid (TPA) (PTA) factory effluent
Reactor: 3 grades of split type adjustable plan fluidized-bed reactors; Reactor volume: 720 liters.
Certain large-scale petrochemical company high concentration terephthalic acid (TPA) (PTA) factory effluent, mainly contain benzene two dioctyl phthalate, acetate, methyl acetate etc., COD is 3000-4000mg/l, adopt continued operation, operating temperature is at 15-30 ℃, and the hydraulic detention time of waste water in reactor is 8h, and day output is 2.16 tons of waste water/days, the immobilization particle loadings that contains bacterial strain is 40-50% (volume fraction), and the COD of water is less than 100-200mg/l after treatment.The COD clearance is greater than 95%.
Embodiment 2: the processing of high-concentration printing and dyeing wastewater
Reactor: 3 grades of split type adjustable plan fluidized-bed reactors (1,2,3 grade of different catalysed particulate of tower body filling);
Reactor volume: 2.4 tons.
Certain printing and dyeing mill's high-concentration printing and dyeing wastewater, mainly contain aniline, terephthalic acid (TPA), anthraquinone quasi-aromatic compound etc., COD is 3000-5000mg/l, adopt continued operation, operating temperature is at 6-25 ℃, and the hydraulic detention time of waste water in reactor is 10h, day output is 5.76 tons of waste water/days, 1 grade of tower body chemical catalysis particle packing amount is 40-50% (volume fraction), and 2,3 grades of tower body biocatalyst particle loadings are 50% (volume fraction), and the COD of water is less than 100mg/l after treatment.The COD clearance is greater than 97%.
Embodiment 3: the processing of high concentration food and drink waste water
Reactor: 2 grades of split type adjustable plan fluidized-bed reactors; Reactor volume: 500 liters.
Certain large-scale hotel high concentration food and drink waste water, mainly contain protein, fat, starch etc., COD is 2000-5000mg/l, adopt continued operation, operating temperature is at 15-25 ℃, and the hydraulic detention time of waste water in reactor is 6h, and day output is 2 tons of waste water/days, the immobilization particle loadings that contains bacterial strain is 40-50% (volume fraction), and the COD of water is less than 100mg/l after treatment.The COD clearance is greater than 98%.
Embodiment 4: the conversion of fumaric acid
Reactor: 3 grades of split type adjustable plan fluidized-bed reactors; Reactor volume: 2 tons.
Certain biochemical-pharmaceutical factory is converted into fumaric acid with fumaric acid, adopt continued operation, operating temperature is at 25-30 ℃, the hydraulic detention time of fumaric acid solution in reactor is 2h, day output is 24 tons of fumaric acid solution/days, the immobilization particle loadings that contains bacterial strain is 40-50% (volume fraction), and the fumaric acid conversion ratio is greater than 95% after treatment.
Claims (7)
1. split type adjustable plan fluidized-bed reactor, it is characterized in that structure comprises split type tower body, diversing bucket, gas distributor, gas-liquid-solid three phase separator, visor, the diversing bucket adjusting rod, liquid connecting line between tower, gas connection pipe line between tower, the solid discharge mouth, liquid discharge outlet, adjustable diversing bucket is housed in the split type tower body, the diversing bucket upper end is equipped with the diversing bucket adjusting rod, gas-liquid-solid three phase separator is equipped with on split type tower body top, the gas distributor of detachable is equipped with in the bottom of split type tower body, the single tower body bottom of split type tower body is equipped with the solid discharge mouth, and liquid discharge outlet is equipped with in the single tower body lower end of split type tower body.
2. a kind of split type adjustable plan fluidized-bed reactor according to claim 1, it is characterized in that split type tower body is a plurality of tower bodies, each tower body can both move individually, a plurality of tower body combined runnings, load the catalyst granules of dissimilar and different loadings separately according to operating condition, feed different reacting gas and liquid, simultaneously the fluidisation area and the settling zone of the single tower body of free adjustment.
3. a kind of split type adjustable plan fluidized-bed reactor according to claim 1 is characterized in that the ratio of height overall and the internal diameter of single tower body of the single tower body of split type tower body is 6-12, and the diversing bucket diameter is 0.3-0.6 with the ratio of the internal diameter of single tower body.
4. a kind of split type adjustable plan fluidized-bed reactor according to claim 1 is characterized in that the diversing bucket upper end of the single tower body of split type tower body is equipped with the diversing bucket adjusting rod, and adjusting rod is 2 screw rods; Diversing bucket adjusting rod top is connected with gas-liquid-solid three phase separator, but the position of free adjustment diversing bucket.
5. a kind of split type adjustable plan fluidized-bed reactor according to claim 1 and 2 is characterized in that the distance of following end distance gas distributor of diversing bucket of the single tower body of split type tower body is 0.5-1.5 with interior diversing bucket diameter ratio; The distance of the gas-liquid-solid three phase separator of upper end distance of diversing bucket is 1-3 with interior diversing bucket diameter ratio; The single tower body of split type tower body two ends is up and down installed visor; The lower end visor is 0.5-1 apart from the distance of gas distributor upper end with interior diversing bucket diameter ratio, and the upper end visor is 1-1.5 apart from the distance of gas-liquid-solid three phase separator with interior diversing bucket diameter ratio.
6. a kind of split type adjustable plan fluidized-bed reactor according to claim 1 and 2, it is characterized in that device has the liquid connecting line between the tower body of split type tower body, a plurality of liquid control valve doors, the liquid between the single tower body of split type tower body is carried by liquid connecting line between tower; By control valve, make single tower body free conversion between in parallel or series connection of split type tower body, and the liquid phase hydraulic detention time of the single tower body of energy free adjustment.
7. a kind of split type adjustable plan fluidized-bed reactor according to claim 1 and 2, it is characterized in that device has the gas connection pipe line between the tower body of split type tower body, a plurality of gas control valves, the gas between the single tower body of split type adjustable tower body can be carried by gas connection pipe line between tower; By control valve, make the gas free conversion between gas of different nature in the single tower body of split type tower body, and air inflow and pressure that can the single tower body of free adjustment.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200410014229.7A CN1256180C (en) | 2004-03-08 | 2004-03-08 | Separated regulatable quasi-fluidized bed reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200410014229.7A CN1256180C (en) | 2004-03-08 | 2004-03-08 | Separated regulatable quasi-fluidized bed reactor |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1559657A CN1559657A (en) | 2005-01-05 |
| CN1256180C true CN1256180C (en) | 2006-05-17 |
Family
ID=34440269
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN200410014229.7A Expired - Fee Related CN1256180C (en) | 2004-03-08 | 2004-03-08 | Separated regulatable quasi-fluidized bed reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1256180C (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101274245B (en) * | 2007-03-28 | 2010-09-01 | 中国石油大学(北京) | Annular space air-lift gas-solid loop flow reactor |
| DE102016210062A1 (en) * | 2016-06-08 | 2017-12-14 | Robert Bosch Gmbh | Fluidized bed system |
-
2004
- 2004-03-08 CN CN200410014229.7A patent/CN1256180C/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| CN1559657A (en) | 2005-01-05 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102745809B (en) | Anaerobic fluidized bed reactor | |
| CN202297249U (en) | Inner-circulated anaerobic fluidize bed reactor | |
| CN2562866Y (en) | Multiple stage circular flow reactor | |
| CN1911835A (en) | Sequential air lifting circulation waste water biological treatment reactor and its process | |
| CN203021355U (en) | Upflow mixed type anaerobic biological membrane reactor | |
| JPS6121727A (en) | Method for performing reaction and mass transfer process in non-uniform fluid system | |
| CN1019794B (en) | Improved bed process | |
| CN1923351A (en) | Staged reactor | |
| CN1171667C (en) | Multi-stage circular flow reactor | |
| CN1301151C (en) | Outside circulation gas lift type membrane reactor | |
| CN1174815A (en) | High-effect anaerobic treatment device for waste water and method thereof | |
| CN1256180C (en) | Separated regulatable quasi-fluidized bed reactor | |
| CN2647845Y (en) | Coking waste water disposal device | |
| CN1025491C (en) | Improved fluidized bed process and apparatus | |
| CN100337936C (en) | Improved bioreactor | |
| CN113083169B (en) | Fluidized bed hydrogenation reactor and using method thereof | |
| CN201785246U (en) | CAFT high-efficiency anaerobe reactor for processing sewage | |
| CN200951395Y (en) | Multiple stage reactor | |
| CN2841645Y (en) | External closed-flow air lift membrance reactor | |
| CN1226201C (en) | Anaerobic/aerobic dual purpose waste water treatment system | |
| CN1199877C (en) | Aerobic-anaerobic air float separation biological fluidized composite reactor | |
| CN1215992C (en) | Up-ward spiral flow bioreactor for sewage treatment and treatment system composed thereof | |
| CN2719834Y (en) | Improved bioreactor | |
| CN2813623Y (en) | Multi-tube external circulating reactor | |
| CN113244860B (en) | Fluidized bed hydrogenation reactor and using method thereof |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| ASS | Succession or assignment of patent right |
Owner name: NANJING POLYTECHNIC UNIV. Free format text: FORMER OWNER: SHEN SHUBAO Effective date: 20050429 |
|
| C41 | Transfer of patent application or patent right or utility model | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20050429 Address after: 210009, 5 new model street, Gulou District, Jiangsu, Nanjing Applicant after: Nanjing University of Technology Address before: 210009, 5 new model street, Gulou District, Jiangsu, Nanjing Applicant before: Shen Shubao |
|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C19 | Lapse of patent right due to non-payment of the annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |